Method for natural gas conversion to high hydrocarbons

FIELD: hydrocarbon manufacturing.

SUBSTANCE: natural gas is brought into reaction with vapor and oxygen-containing gas in at least one reforming zone to produce syngas mainly containing hydrogen and carbon monoxide and some amount of carbon dioxide. Said gas is fed in Fisher-Tropsh synthesis reactor to obtain crude synthesis stream containing low hydrocarbons, high hydrocarbons, water, and unconverted syngas. Then said crude synthesis stream is separated in drawing zone onto crude product stream containing as main component high hydrocarbons, water stream, and exhaust gas stream, comprising mainly remained components. Further at least part of exhaust gas stream is vapor reformed in separated vapor reforming apparatus, and reformed exhaust gas is charged into gas stream before its introducing in Fisher-Tropsh synthesis reactor.

EFFECT: increased hydrocarbon yield with slight releasing of carbon dioxide.

7 cl, 3 dwg, 1 tbl, 5 ex

 

The technical field

The present invention relates to the chemical conversion of natural gas or other suitable fossil fuels into synthetic hydrocarbons (Tintin). In particular, the present invention relates to a system for optimizing the production of synthetic hydrocarbons.

Prior art

Known methods for the conversion of natural gas or other fossil fuels into synthetic hydrocarbons include two stages. First, natural gas or other fossil fuel is converted into synthesis gas, i.e. a mixture consisting primarily of hydrogen and carbon monoxide and some carbon dioxide, and in the second stage, the synthesis gas is converted into synthetic hydrocarbons in the so-called Fischer-Tropsch synthesis. This synthetic hydrocarbon product usually consists of higher hydrocarbons, such as pentane and higher compounds (C5+). This process may also include the additional step in which the crude synthetic hydrocarbon product is subjected to finishing with the delivery of finished products.

There is a method of transforming natural gas into higher hydrocarbons, which contains stage a) reacting natural gas with steam in at least one zone of reforming catalyst p is forming with receiving the first stream of synthesis, containing carbon monoxide, carbon dioxide and hydrogen; C) passing the first stream of synthesis without separation of carbon dioxide into the reactor Fischer-Tropsch process to obtain a second stream of synthesis with hydrocarbon and carbon dioxide; (C) passing the second stream in the zone of extraction, which extracts the desired higher hydrocarbon products, and the remaining components form a third stream; e) passing at least a portion of the third stream in a reforming zone of the first stage of the process - the European patent EP 0516441 A1. However, this process does not contain the introduction phase of the waste gas stream subjected to reforming in the gas stream prior to its submission to the synthesis reactor on stage).

A method of obtaining C5+hydrocarbons, which describes the stages a) catalytic steam reforming of C4 hydrocarbons to obtain synthesis gas under appropriate temperature and pressure; C) catalytic conversion of synthesis gas into hydrocarbons under appropriate temperature and pressure in the presence of a catalyst Fischer-Tropsch process; (C) partial evaporation of the water obtained in stage b) under certain temperature and pressure using a hot gas environment; d) further heating the gas mixture obtained in stage C); (e) the introduction of at least part of the remaining water in the hot gas mixture; W) use the of gas mixtures as raw materials for the stream reforming stage a) Patent England GB-A-2223029. However, the disadvantage of this method is low efficiency for carbon and low thermal efficiency.

Synthesis gas for the production of synthetic hydrocarbons, as mentioned above, usually obtained by steam reforming or partial combustion, or a combination of these two processes. In the production of synthesis gas also plays an important role in the reaction of conversion of water gas. These reactions can be written as follows:

1) steam reforming of CH4+H2O=CO+3H2O ΔH=206 kJ/mol

2) partial combustion of CH4+1,5O2=CO+2H2About ΔH=-519 kJ/mol

3) conversion of water gas CO+H2O=CO2+H2ΔH=-41 kJ/mol

The Fischer-Tropsch synthesis for production of synthetic hydrocarbons can be written as follows:

4) the Fischer-Tropsch synthesis CO+2H2=[-CH2-]+H2O ΔH=-167 kJ/mol, where [-CH2-] represents the basic structural unit in the molecules of hydrocarbons. The Fischer-Tropsch synthesis is a highly exothermic process, so the heat transfer is essential when designing a reactor for this process.

An important parameter when determining the maximum output of synthetic hydrocarbons is the stoichiometric number (MF), which is defined as clicks the zoom:

5) MF=(H2-CO2)/(CO+CO2)

In theory, the output of synthetic hydrocarbons is maximum when MF=2,0, when not react further with the formation of CO2after conversion of water gas (equation 3). In this case, the relation of H2/CO is equal to MF, that is, 2,0, at which theory is obtained the maximum yield of synthetic hydrocarbons according to equation (4). However, in practice, when receiving the synthesis gas will always occur to some extent, the conversion of water gas, so that the output FROM the and result of the release of hydrocarbons becomes a little lower.

Moreover, the maximum yield of synthetic hydrocarbons effectively achieved when several smaller ratio of H2/CO, typically about 1.6 to 1.8. When the ratio of H2/CO equal to 2.0 or more, the output of synthetic hydrocarbons will be reduced because of the larger methane and other lower hydrocarbons (C4-), which are usually undesirable products.

The preferred technology for production of synthetic hydrocarbons from synthesis gas is a non-catalytic partial oxylene (ROCH) or Autoterminal reforming (ATR), in which partial combustion is combined with the adiabatic catalytic steam reforming (equation 1) in the same reactor block.

Another technologyrelated a combined reforming tubular reactor for catalytic steam reforming followed Autoterminal reforming.

A desirable ratio of H2/CO is achieved by operating the reactor to produce synthesis gas in combination mode with a low steam/carbon and high temperature, in addition to the recirculated part of the exhaust gases with a high content of CO2with stage Fischer-Tropsch synthesis in a reactor synthesis gas, in order to limit the flow of the conversion of water gas. Thus, the relation of H2/CO will be closer to the specified value CQ.

A disadvantage of the known technologies for producing synthetic hydrocarbons is low efficiency on carbon compared with theoretical value. The effectiveness of the carbon is defined as the relationship between the total carbon content in the crude synthetic hydrocarbon product and the total carbon content in the original natural gas. Thus, the efficiency of the carbon is an indicator of the actual conversion of carbon materials in the final product and the percentage of the conversion of raw materials in CO2. When the low efficiency of the carbon setting gives a small yield of the product and a large selection of CO2that creates problems for the environment.

As mentioned above, the catalytic Autoterminal the non-catalytic reforming and partial oxidation are the preferred technology PR is the production of synthesis gas for the Fischer-Tropsch synthesis. When using natural gas as raw materials in these methods, the formed synthesis gas having the value of MF is usually in the range of from 1.6 to 1.8, which achieved the highest yield of synthetic hydrocarbons directly into the reactor Fischer-Tropsch synthesis. However, this value is lower midrange two, what to plant in General means lower efficiency on carbon (compared to that which can be achieved in theory) because of the shortage of hydrogen.

The combined reforming, which usually takes place in a tubular reactor for catalytic steam reforming followed by a second reforming reactor with oxygen, is capable of producing synthesis gas with a midrange value of 2.0, which in theory should achieve the highest efficiency for the carbon plant producing synthetic hydrocarbons. However, the actual effectiveness of the carbon will not be above that which is achieved by using a non-catalytic partial oxidation or catalytic Autoterminal reforming, because of the high degree of recirculation of exhaust gases in the synthesis reactor, which is required to limit the conversion of water gas, compared with the catalytic Autoterminal reforming as a result of increased relationships steam/carbon and due to low yield of the desired higher synthetically the hydrocarbons when such is CQ.

Thus, the aim of the present invention to provide an improved method for the conversion of natural gas or other fossil fuels in higher hydrocarbons, which overcome the above-mentioned disadvantages of the known methods.

Disclosure of the invention

According to the present invention this objective is achieved in the way of turning natural gas or other fossil fuels in higher hydrocarbons, which involves the following stages:

a) interaction of natural gas with steam and oxygen-containing gas in at least one reforming zone to obtain synthesis gas, which consists mainly of H2and, apart from a small amount of CO2;

b) feeding the synthesis gas in the reactor Fischer-Tropsch synthesis, to obtain a raw stream of synthesis consisting of lower hydrocarbons, higher hydrocarbons, water and neprevyshenie synthesis gas;

c) a separation zone extraction of the specified raw stream of synthesis on the flow of the crude product, which mainly contains the lower hydrocarbons, higher hydrocarbons, water flow and the flow of exhaust gases, which mainly contains the remaining components, characterized in that the method also comprises the stage of:

d) steam reforming at least part of the flow of exhaust gases in a separate apparatus vapor is th reforming;

e) introduction of the exhaust gas subjected to reforming in the gas stream prior to its submission to the reactor Fischer-Tropsch synthesis.

The term “lower hydrocarbons” refers to hydrocarbons With a1-C4. The term “higher hydrocarbons” refers to hydrocarbons C5+.

Preferably, the steam reforming stage d) is carried out in conditions that are favorable for the conversion of CO2in WITH in the reversible reaction of conversion of water gas.

Moreover, it is also preferable to gidrirovanii the portion of the exhaust gases, which is subjected to steam reforming, in order to saturate any unsaturated hydrocarbons to stage d).

In a preferred variant embodiment of the natural gas fed into the reactor steam reforming stage d) together with the supply of the exhaust gas.

In a preferred variant embodiment of the exhaust gas after reforming is introduced into the gas stream after stage a), but before stage b).

In another preferred variant of embodiment of the exhaust gas after reforming is introduced into the gas stream prior to stage a).

Also preferably, the portion of the flue gas after reforming was injected into the gas stream prior to stage a)as part of the gases were introduced after stage a), but before stage b).

The application of the method of the present invention provides certain advantages over the known methods.

When about is the introduction of the reformer and the exhaust gas recirculation is possible the following:

The magnitude of MF from the normal of 1.6-1.8 for ATR to approximately 2.0.

- Maintain or increase output, so that the ratio H2/CO is close to the value of CQ.

- Achievement relationship of H2/WITH less than 2.0 in place of the entrance to the reactor Fischer-Tropsch synthesis, which is achieved by the increased yield of higher hydrocarbons.

The method according to the invention provides increased efficiency for carbon and high thermal efficiency. This leads to a reduction in the allocation of CO2that it is desirable for environmental and economic reasons. The consumption of oxygen in the method according to the invention is smaller than in the case of traditional plants for the production of synthesis gas using ROCH or ATR, which causes the reduction of capital costs and reducing energy consumption.

In addition, it is possible to achieve operational advantages, such as improved stability due to the operation of the reactor synthesis gas, oxygen supply for combustion, at a somewhat lower temperature compared to the temperature in the case of the use of technology of the prior art. Increased amounts of methane (reduced conversion of natural gas) in this case will turn into the reforming reactor off-gas.

By moving the recirculation of exhaust gas into the main section of the reactor is Intesa gas can also reduce the size of the equipment and thereby reduce costs in this section.

Below the invention will be explained in more detail with reference to accompanying drawings.

Figure 1 is a simplified process diagram illustrating a method of production of synthetic hydrocarbons by the method of the invention.

Figure 2 is a more detailed process diagram illustrating a first preferred variant of the method according to the invention.

Figure 3 is a more detailed process diagram illustrating the second preferred variant of the method according to the invention.

A simplified process diagram figure 1 shows a method of production of synthetic hydrocarbons with the use of natural gas as the primary source of carbon and hydrogen, while figures 2 and 3 presents a more detailed process flow diagrams, showing two preferred variant of this method.

The method of Fischer-Tropsch synthesis according to the invention, based on natural gas or other fossil fuels, can be subdivided into three main parts, i.e. the first part for the production of synthesis gas, the second part for the Fischer-Tropsch synthesis and the third part for the reformer off-gas from a Fischer-Tropsch synthesis.

The production of synthesis gas

Natural gas is delivered for installation in the main line 1 natural gas. the beginning of the natural gas is heated, usually approximately 350-400°With, before passing through the desulfurization unit 20. In this unit, sulfur, present in natural gas in the form of various organic compounds into hydrogen sulfide in the contact with a suitable hydrogenation catalyst. Then the content of hydrogen sulfide is reduced to the desired level through the use of a layer of zinc oxide.

After desulfurization in the gas add water vapor to provide the desired ratio between water vapor and carbon (pairs/Sec), usually from approximately 0.6 to 1.3, for the production of synthetic hydrocarbons. The mixture of the gas with water vapor is heated and injected into the reactor pre-reformer 3, in which the hydrocarbons2and above is converted into methane, co and CO2. Typically, the operating temperature in the reactor pre-reformer 3 is in the range from 430 to 500°C. the reactor pre-reformer can be excluded, particularly when using natural gas with a low content of hydrocarbons of C2+ and above.

The hydrogen required in the desulfurization unit 20 and the reactor pre-reformer 3, is added to natural gas before it enters the desulfurization unit 20. As shown in the figures, part of the off-gas containing hydrogen, among other components, can be recycled and dobavlat is camping in the gas before entering the desulfurization unit 20. In addition, you can extract hydrogen from the specified exhaust gas, for example in the process of adsorption with pressure jump (PSA) or the hydrogen may come from another source.

Then the gas mixture after the preliminary reactor reforming additionally heated to a temperature usually 550-650°With, before, in the reactor Autoterminal reforming (ATR) 5 together with oxygen or oxygen-containing gas, such as air, which is supplied by an oxygen pipe 4, usually from cryogenic oxygen plants (not shown). Then the gas enters (ATR) 5, is converted into synthesis gas in the reactor ATR 5 as a result of partial combustion in the upper part of the reactor and process of steam reforming of gases at the Nickel catalyst in the lower part of the reactor ATR 5. Typically, the formation of synthesis gas in ATR flows under pressure for about 30-40 bar, and the temperature of the gas at the outlet of ATR 5 is typically in the range of 950-1050°C.

Hot synthesis gas leaving the ATR 5 via line 6 synthesis gas is first cooled in heat exchanger 22, in which water from the inlet pipe 21, it usually turns into high-pressure steam at the outlet 23. The figures shows one heat exchanger, but in practice you can use a variety of heat exchangers connected in series, in which the synthesis gas is cooled to lemoi temperature. Typically, the gas is cooled to a temperature of 40-70°when using cooling water.

Then the condensed water separated from the synthesis gas to feed gas into the reactor 7 of the Fischer-Tropsch synthesis.

The Fischer-Tropsch synthesis

The desired synthetic hydrocarbons are formed in a known manner in the reactor 7 Fischer-Tropsch process, in which hydrogen and carbon monoxide is converted into higher hydrocarbons with the formation of water as a by-product in accordance with the above equation (4). The reactor 7 Fischer-Tropsch usually works under the pressure of 20-40 bar at a temperature of 180-240°C. Since the reaction is exothermic, heat is usually removed from the reactor 7 due to the formation of steam at an intermediate pressure, typically about 5-20 bar.

The product stream from the reactor Fischer-Tropsch 7 typically contains the desired product in the form of hydrocarbons C5+, by-products in the form of lower hydrocarbons (C5-), CO2H2O, and unreacted synthesis gas, i.e. WITH and H2. This product stream is separated in the extraction block product 24 to the flow of the crude product, containing mainly the desired hydrocarbons and outgoing line 25; selected water coming through the line 26; and the flow of exhaust gas, containing mainly the above by-products and unreacted synthesis gas, hadashi on line 9.

In turn, the exhaust gas in the respective line 9 is divided into three streams. The first part passes through the recirculation line 10 and is compressed in the compressor 27 to provide recycling to the stage of synthesis gas production, as shown below; the second part passes through the reformer 12 to the stage of the reformer off-gas, while the third part is discharged through the discharge line pressure 11 and, if necessary, is used as fuel in those nodes of the process, which consumes heat.

The reformer off-gas

The exhaust gas in the respective lines 12 is preferably first supplied to the reactor 28 hydrogenation of exhaust gas to progenerate any unsaturated hydrocarbons. Working temperature of the hydrogenation reactor 28 is typically 220-250°while the working pressure is approximately 20-40 bar. This reactor 28 hydrogenation of the exhaust gas is not necessarily preferred, however, unsaturated hydrocarbons have an increased tendency towards coking compared to saturated hydrocarbons during subsequent high temperature processing.

After hydrogenation in reactor 28 in the exhaust gas add water vapor and possibly some amount of natural gas, respectively, in the input line pair 13 and the strip 14, to the heated gas in the reactor 1 of the reformer off-gas, where light hydrocarbons are subjected to steam reforming to form CO and hydrogen (see equation 1), while present in flue gas CO2turns into in the reverse reaction the conversion of water gas (according to equation 3). The flow of raw natural gas can be extracted from the product stream leaving the reactor pre-reformer 3 (net splitting).

Operating temperature in the reactor reformer off-gas typically exceeds 800°C, preferably from 850 to 950°Since, while the working pressure is usually from 10 to 40 bar. If necessary, different operating pressure in the reactor reformer flue gas and the Fischer-Tropsch synthesis is possible to provide a compressor after the reactor reformer off-gas. The heat required for these processes can be achieved by combustion of fuel, which may be a small part of the off-gas from the discharge line pressure 11.

Depending on the hydrocarbon content of C2+ in the gas which can be added to the input line of the gas 14 may be necessary in the installation of the reactor pre-reforming after adding water vapor to the inlet of the reactor reformer off-gas. Such reactor preliminary reformer is of the same type as the reactor 3, and destined the items for the conversion of ethane and higher hydrocarbons in the gas stream in a methane co and CO 2resulting eliminates/reduces the coking at high temperatures. If the input 14 not added natural gas, or natural gas with a methane content of 90% or more, in this way usually do not require reforming reactor.

Then a hot stream of exhaust gas after reactor 15 reformer off-gas can be cooled in the heat exchanger 30, which is received through the inlet 31, the water turns into water vapor, which exits through the steam pipe 32. On the figures specified one heat exchanger, but in practice there may be a variety of heat exchangers connected in series, in which the synthesis gas is cooled to the desired temperature. Then the condensed water is separated from the exhaust gas from the reforming reactor, prior to compression of the gas in the compressor 33, which is directed along the line of the exhaust gas 16 in line synthesis gas 6, before entering the reactor Fischer-Tropsch synthesis. You can also enter the exhaust gas after reforming directly in the gas flow between the reactor pre-reformer 3 and the reactor 5 Autoterminal reforming (ATR). In addition, there is the possibility of splitting the flow of the exhaust gas after reforming with the direction of one component of the flow in the reactor 7 of the Fischer-Tropsch synthesis, and the other is about average flow in ATR 5.

The flow of exhaust gas after reforming goes in ATR 5 to implement additional steam reforming education in the reverse reaction the conversion of water gas, as the temperature in the ATR reactor 5 is higher than the temperature in the reactor reformer off-gas, thus achieving high efficiency installation on carbon. This effect may be partly weakened due to the combustion of CO and hydrogen to carbon dioxide and water. The decision in this case and any other cases related to the quantity of exhaust gas, will depend on a number of operational parameters.

According to the invention the main purpose of reforming and recirculated exhaust gas is steam reforming of lower hydrocarbons to CO and hydrogen, resulting in increased stoichiometric number (MF) to the desired value of 2.0, which is an important condition to achieve significantly higher efficiency of the facility. Because the exhaust gas contains a bit of light hydrocarbons, steam reforming only this thread will give only a slight increase efficiency. Therefore, the addition of natural gas or other source of lower hydrocarbons through a gas input 14 will result in an additional increase efficiency on carbon.

Another advantage of the om adding natural gas to the reforming reactor off-gas is reduced quantity of raw material gas, supplied in ATR.

The combined system

In sum, the method of the present invention provides significant and important increase in the efficiency of carbon, reduces oxygen consumption and improves the economic performance of the installation.

Using the reformer and the recycling of a significant part of the exhaust gas in the reactor Fischer-Tropsch synthesis 7 and/or ATR 5, you can reduce the size of the equipment in the resource section of the ATR unit, compared to those needed in the case when the exhaust gas must be recycled to the hydrogenation unit 28, as in modern installations.

The exhaust gas from section 24 of the extraction product, as mentioned above, is divided into three parts. It is established that it is advantageous to recycle 0-20%, for example, approximately 10% of the gas in the hydrogenation unit 28; using 0-40%, for example, about 30%, as a fuel reforming reactor off-gas; and use 40-80%, for example, about 60%, as a raw material in the reactor reformer off-gas of this method.

Examples

Simulated five different settings/modes of operation, in order to show the advantages of the present invention as compared with previously known technology, which has traditionally been used in plants for the synthesis of synthetic hydrocarbons. In all examples, the production was 20,000 barrels/day the Lee 101 tons/hour.

These examples are presented below:

Example: Production of synthetic hydrocarbons traditional Autoterminal reforming (ATR).

Example: Production of synthetic hydrocarbons traditional combined reforming.

Example: Production of synthetic hydrocarbons using ATR and reactor reformer off-gas to the Fischer-Tropsch synthesis. There is no adding of natural gas in the reforming reactor off-gas. The product from the reforming reactor off-gas enters the reactor Fischer-Tropsch synthesis.

Example D: the Production of synthetic hydrocarbons using ATR and reactor reformer off-gas to the Fischer-Tropsch synthesis. In the reforming reactor off-gas are added directly to 10% of natural gas as raw material process. The product from the reforming reactor off-gas enters the reactor Fischer-Tropsch synthesis. Part of the exhaust gas that is diverted from the plant, is used as fuel gas in the reformer off-gas.

Example E: the Production of synthetic hydrocarbons using ATR and reactor reformer off-gas to the Fischer-Tropsch synthesis. In the reforming reactor off-gas are added directly to 20% of natural gas as raw material process. The product from the reforming reactor from tamago gas enters the reactor ATR. Some of the natural gas (3%) is used as fuel in the reformer off-gas, together with part of the exhaust gas, which is removed from the installation. The crude product is a natural gas of the following composition:

CO21,84%
Nitrogen0,36%
Methane80,89%
Ethan9,38%
Propane4,40%
Bhutan2,18%
Pentane0,62%
Hexane0,22%
Octane0,11%

In the simulation were obtained the following results related to the most important key data:

Table
Example A,The example InExampleExampleExample
comparativeComparativeDE
Raw materials - natural gas77677790715070627070
KMOL/h      
Pairs/in line With the synthesis gas0,61,80,60,60,6
Oxygen consumption45903289380133993290
t/d     
The share of off-gas4025303030
synthesis f-T     
used as     
fuel from all     
flue gas%     
The share of off-gas6075999
synthesis f-T, added     
for ATR, from su is th      
flue gas%     
The share of off-gas synthesis f-T, added  616161
to the flue gas reforming, all the exhaust gas,%     
Pairs/S3in the exhaust gas  5,31,00,6
reforming     
CO2/C3in the exhaust gas  5,31,00,6
reforming     
Outlet temperature  900900900
off-gas     
reforming,°     
Efficiency71,070,977,178,077,9
Carbon1,%     
Thermalto 59.459,264,665,365,3
efficiency2,%     
Emissions of CO2t/h127,11128,3992,5087,4688,00

1The effectiveness of the carbon=carbon content in the crude synthetic product, referred to the total carbon content in the original natural gas.

2Thermal efficiency=lower calorific value (i.e. calorific value, obtained by complete combustion) of the crude synthetic product/lower calorific value only source of natural gas.

3Organic carbon

From the above table clearly see the advantages of using the present invention (examples C, D and E) compared with previously known to the persons (examples a and b).

For the same quality product in the method of the present invention reduces the consumption of natural gas by approximately 8-10%, which in turn, directly affects the efficiency of the carbon and thermal efficiency for the method of the invention is significantly higher than when using previously known methods.

Another important effect, which is clearly seen from the above results, a significant reduction of carbon dioxide emissions at the same performance on synthetic hydrocarbons. As you can see from the table above, the carbon dioxide emissions when using the method of the invention is approximately 40% lower than when using traditional methods.

Oxygen consumption in the sample, which represents the method according to the prior art, is the lowest among the simulated examples. Although low oxygen consumption is a positive factor, results in important parameters, i.e. the efficiency of the carbon and thermal efficiency, significantly weaker than in the case of the present invention, i.e. examples C, D and E.

The present invention is described for the case of the use of natural gas as a carbon source. However, this method can be used for all types of gas, the cat is, which contains significant amounts of lower hydrocarbons, as well as other types of fossil fuels, and the possible combinations of different carbon sources.

1. The method of conversion of natural gas or other fossil fuels in higher hydrocarbons, which comprises the following stages:

a) interaction of natural gas with steam and oxygen-containing gas in at least one reforming zone to obtain synthesis gas, which consists mainly of H2and WITH the addition of a certain amount of CO2;

(b) the specified synthesis gas is sent to the reactor Fischer-Tropsch synthesis to obtain a raw stream of synthesis consisting of lower hydrocarbons, higher hydrocarbons, water and neprevyshenie synthesis gas;

c) a separation zone extraction of the specified raw stream of synthesis on the flow of the crude product, which mainly contains the lower hydrocarbons, higher hydrocarbons, water flow and the flow of exhaust gases, which mainly contains the remaining components

characterized in that the method also comprises the stage of:

d) steam reforming at least part of the flow of exhaust gases in a separate apparatus steam reforming;

e) introduction of the exhaust gas subjected to reforming in the gas stream prior to its submission to the reactor Fischer-Tropsch synthesis.

2. The method according to claim 1, characterized in, that the temperature of the process steam reforming stage d) exceeds 800°C., preferably from 850 to 950°C.

3. The method according to claim 1 or 2, characterized in that a part of exhaust gases, which is subjected to steam reforming, also hydronaut in order to saturate any unsaturated hydrocarbons to stage d).

4. The method according to any of the preceding paragraphs, characterized in that the natural gas is fed into the steam reforming reactor in stage (d) together with the supply of the exhaust gas.

5. The method according to any of the preceding paragraphs, characterized in that the exhaust gas after reforming is introduced into the gas stream after stage a), but before stage b).

6. The method according to any one of claims 1 to 4, characterized in that the exhaust gas after reforming is introduced into the gas stream prior to stage a).

7. The method according to any one of claims 1 to 4, characterized in that a part of exhaust gas after reforming is introduced into the gas stream prior to stage a)as part of the gases is introduced after stage a), but before stage b).



 

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3 cl, 3 tbl, 6 ex

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SUBSTANCE: natural gas is brought into reaction with vapor and oxygen-containing gas in at least one reforming zone to produce syngas mainly containing hydrogen and carbon monoxide and some amount of carbon dioxide. Said gas is fed in Fisher-Tropsh synthesis reactor to obtain crude synthesis stream containing low hydrocarbons, high hydrocarbons, water, and unconverted syngas. Then said crude synthesis stream is separated in drawing zone onto crude product stream containing as main component high hydrocarbons, water stream, and exhaust gas stream, comprising mainly remained components. Further at least part of exhaust gas stream is vapor reformed in separated vapor reforming apparatus, and reformed exhaust gas is charged into gas stream before its introducing in Fisher-Tropsh synthesis reactor.

EFFECT: increased hydrocarbon yield with slight releasing of carbon dioxide.

7 cl, 3 dwg, 1 tbl, 5 ex

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